Classifications

• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C17/00—Preparation of halogenated hydrocarbons
  • C07C17/25—Preparation of halogenated hydrocarbons by splitting-off hydrogen halides from halogenated hydrocarbons

Definitions

• the present invention relates to a process for the production of a fluorine containing olefin and more particularly to a process for the production of trifluoroethylene.
• a process for the production of a fluorine containing olefin which process comprises passing a gaseous feed comprising a saturated hydrohalocarbon reactant having a fluorine substituent and one or more further halogen substituents through a heated reaction zone in which there is contained a Lewis acid catalyst.
• a gaseous feed comprising a saturated hydrohalocarbon reactant having a fluorine substituent and one or more further halogen substituents is passed through a heated reaction zone where it is subjected to a dehydrohalogenation reaction in the presence of a Lewis acid catalyst so as to yield the desired fluorine containing olefin.
• the process of the present invention may be used to prepare a variety of fluorine containing olefins, but is particularly concerned with the production of fluorine containing ethylenes and more specifically with the production of trifluoroethylene.
• Fluorine containing ethylenes are prepared by subjecting a hydrohaloethane starting material containing a fluorine substituent and one or more further halogen substituents to the process of the present invention.
• the one or more further halogen substituents contained in the hydrohaloethane may be fluorine, chlorine, bromine and/or iodine atoms, but will preferably be fluorine and/or chlorine atoms and more preferably will be exclusively fluorine atoms.
• the hydrohaloethane starting material is preferably one of 1,1,1,2-tetrafluoroethane (hereinafter R-134a) and 1,1,2,2-tetrafluoroethane (hereinafter R-134), and more preferably is R-134a.
• the heated reaction zone may be provided by any suitably configured reactor vessel.
• the heated reaction zone is provided by a heated tube reactor.
• the reactor vessel should, of course, be made of a thermally conductive material which is stable, i.e. will not decompose or melt, at the elevated temperatures and under the chemical environment prevailing during operation of the process.
• the reactor vessel may, for example, be made of carbon, graphite or a conductive metal or metal alloy such as nickel and its alloys. It has been found that reactor vessels made of nickel are particularly efficacious in the process of the present invention.
• Suitable Lewis acid catalysts for the present process include chromia (Cr 2 O 3 ) and materials comprising chromia which has been doped with a metal, possibly in the form of a metal compound.
• Suitable metals for doping the chromia include nickel, cobalt, zinc, iron and copper, especially zinc.
• Suitable catalysts are the fluorine containing Lewis acids such as aluminium fluoride (AlF 3 ) and materials comprising a fluorine containing Lewis acid which has been doped with a metal, possibly in the form of a metal compound.
• Suitable metals for doping the fluorine containing Lewis acid include nickel, cobalt, zinc, iron and copper, especially iron.
• Preferred catalysts are those comprising a fluorine containing Lewis acid and catalysts comprising aluminium fluoride are especially preferred.
• the catalyst may be compressed into pellets and used in a fixed bed or, alternatively, it may be used in particulate form in a fluidised bed. Mixtures of two or more different catalysts may also be used in the process of the present invention.
• the catalyst will tend to lose its activity after a time, but spent catalyst may be regenerated by heating it in air at a temperature in the range of from 500° to 1000° C., more preferably in the range of from 600° to 1000° C.
• reaction temperatures in the range of from 350° to 1200° C. are generally employed, with reaction temperatures in the range of from 350° to 1000° C. being preferred.
• reaction temperature employed is preferably in the range of from 350° to 800° C. and more preferably in the range of from 400° to 600° C.
• the residence time for the hydrohalocarbon reactant in the reaction zone is generally in the range of from 0.01 to 100 seconds, with residence times in the range of from 0.1 to 10 seconds being preferred.
• the residence time for the R-134 or R-134a reactant in the reaction zone is preferably in the range of from 0.1 to 7 seconds and more preferably in the range of from 0.3 to 5 seconds.
• residence time we mean the residence time as calculated at room temperatures and pressures (RTP) in accordance with the equation below. ##
• the volumetric fluid flow rate it is necessary to take into account all the fluids which are to be fed to the reactor vessel.
• the process of the present invention may, of course, be operated so that the hydrohalocarbon reactant is the only fluid being charged to the reactor vessel, in which case only the flow rate of this fluid needs to be considered.
• the process of the present invention employs a gaseous diluent (discussed hereinafter) in addition to the hydrohalocarbon reactant
• the volumetric fluid flow rate will be a measure of the total volume of diluent and hydrohalocarbon reactant (in ml) being fed to the reactor vessel per second.
• the gaseous feed entering the reaction zone may be composed entirely, or substantially entirely, of the hydrohalocarbon reactant, it will preferably also comprise an inert diluent gas or vapour which is stable at the elevated temperatures and under the chemical environment prevailing during operation of the process.
• diluent gases/vapours include nitrogen, carbon dioxide, carbon tetrafluoride, steam and superheated steam.
• superheated steam is employed as the diluent, it may be possible to achieve and maintain the desired reaction temperature without using separate heating means.
• the preferred diluent gas is nitrogen.
• the volume ratio of the diluent to the hydrohalocarbon reactant in the gaseous feed entering the reaction zone is preferably in the range of from 1:1 to 20:1, more preferably in the range of from 2:1 to 9:1 and particularly preferably in the range of from 4:1 to 9:1.
• the reaction pressure employed in the process of the present invention is not normally critical and may be atmospheric, sub-atmospheric, or super-atmospheric. However, operating pressures in the region of atmospheric pressure are preferred and, in general, operation at atmospheric pressure or substantially atmospheric pressure is particularly preferred.
• the heating of the reactor vessel to generate the required reaction temperature may be accomplished by any suitable heating means.
• heating may be achieved by electromagnetic induction or by means of a furnace disposed around the reactor vessel.
• it may be possible to generate the required reaction temperature in the reaction zone using a superheated diluent gas or vapour.
• the hot gas stream emerging from the reactor vessel is normally quench cooled.
• the crude material which is obtained from the present process may be treated and purified by conventional techniques (e.g. distillation) in order to isolate and collect the fluorine containing olefin.
• Any unreacted starting material collected from the process may be recycled to the entry side of the reactor vessel and passed through the reaction zone once again in order to improve conversion.
• TriFE trifluoroethylene
• the reactor vessel comprised a piece of nickel tubing of length 15 cms, internal diameter 0.21 cms and external diameter 0.45 cms. This reactor tube was conditioned first of all by heating it at 800° C. while passing a gaseous feed containing 90% by volume of nitrogen and 10% by volume of R-134a through the central reaction zone at a rate of 50 ml/minute. This process was continued for a total of 4 hours.
• the reactor tube was ready for the experimental work.
• a piece of steel gauze was compressed and inserted into the reactor tube in order to retain the catalyst.
• the catalyst was then placed in the reactor tube and the gas feeds (nitrogen diluent and R-134a), which were controlled by means of mass flow controllers, were set and measured using a bubble flow meter.
• the gas feeds were thoroughly mixed together using a static mixer before being passed into the reactor tube.
• the reactor tube was then gradually heated to the desired reaction temperature (400° to 600° C.) using a tube furnace and while the furnace was warming up samples of the feed stream emerging from the mass flow controllers were taken and analysed in order to accurately determine the feed concentration.
• the gaseous product stream emerging from the reactor tube was passed through a caustic scrubber before being sampled and analysed in order to remove any hydrogen fluoride which it might contain.
• TriFE from R-134a The above described general procedure was used to prepare TriFE from R-134a.
• the catalyst used was aluminium fluoride which had been previously dried by heating it to 250° C. in a stream of nitrogen for 3 hours. 0.45 g of the aluminium fluoride catalyst was loaded into the reactor tube and the flows of nitrogen and R-134a were then started and adjusted so that the gaseous feed entering the reactor tube contained 97.58% by volume of nitrogen and 2.42% by volume of R-134a.
• the reactor tube was initially heated to a temperature of 500° C. and during the course of the experiment this temperature was increased to 550° C. and then finally to 600° C. At each temperature, a sample of the gaseous product stream emerging from the scrubber was collected and analysed once the system had equilibriated.
• TriFE from R-134a The above described general procedure was used to prepare TriFE from R-134a.
• the catalyst used was aluminium fluoride which had been previously dried by heating it to 250° C. in a stream of nitrogen for 3 hours. 0.45 g of the aluminium fluoride catalyst was loaded into the reactor tube and the flows of nitrogen and R-134a were then started and adjusted so that the gaseous feed entering the reactor tube contained 92.0% by volume of nitrogen and 8.0% by volume of R-134a.
• the temperature of the reactor tube was raised to 600° C. and once this temperature had been attained the time was set at zero and monitoring of the reaction process began with samples of the gaseous product stream emerging from the scrubber being collected at various times and analysed by gas chromatographic mass spectroscopy.
• Example 2 The above described general procedure was used to prepare TriFE from R-134a.
• the catalyst used in Example 2 was regenerated while in situ in the reactor by heating it to 600° C. in a continuous flow of air for approximately 3 hours. At the end of the regeneration, the catalyst was allowed to cool in a flow of nitrogen. Once the catalyst had cooled, the flows of nitrogen and R-134a were started and adjusted so that the gaseous feed entering the reactor tube contained 92.0% by volume of nitrogen and 8.0% by volume of R-134a.
• the temperature of the reactor tube was raised to 600° C. and once this temperature had been attained the time was set at zero and monitoring of the reaction process began with samples of the gaseous product stream emerging from the scrubber being collected at various times and analysed by gas chromatographic mass spectroscopy.
• the above described general procedure was used to prepare TriFE from R-134a.
• the catalyst used was a blend of aluminium fluoride doped with iron in the form of an iron compound.
• the catalyst was dried prior to use by heating it to 250° C. in a stream of nitrogen for 3 hours. 0.70 g of the catalyst was loaded into the reactor tube and the flows of nitrogen and R-134a were then started and adjusted so that the gaseous feed entering the reactor tube contained 93.0% by volume of nitrogen and 7.0% by volume of R-134a.
• the reactor tube was initially heated to a temperature of 450 ° C. and during the course of the experiment this temperature was increased in stages to 475° C., 500° C. and then finally to 525° C. At each temperature, a sample of the gaseous product stream emerging from the scrubber was collected and analysed once the system had equilibriated.
• the above described general procedure was used to prepare TriFE from R-134a.
• the catalyst used was a blend of aluminium fluoride doped with iron in the form of an iron compound.
• the catalyst was dried prior to use by heating it to 250° C. in a stream of nitrogen for 3 hours. 0.40 g of the catalyst was loaded into the reactor tube and the flows of nitrogen and R-134a were then started and adjusted so that the gaseous feed entering the reactor tube contained 93.5% by volume of nitrogen and 6.5% by volume of R-134a.
• the temperature of the reactor tube was raised to 500° C. and once this temperature had been attained the time was set at zero and monitoring of the reaction process began with samples of the gaseous product stream emerging from the scrubber being collected at various times and analysed by gas chromatographic mass spectroscopy.
• TriFE from R-134a The above described general procedure was used to prepare TriFE from R-134a.
• the catalyst used was a zinc on chromia catalyst (3% by weight of zinc) which had been previously dried by heating it to 250° C. in a stream of nitrogen for 3 hours. 0.50 g of the catalyst was loaded into the reactor tube and the flows of nitrogen and R-134a were then started and adjusted so that the gaseous feed entering the reactor tube contained 93.54% by volume of nitrogen and 6.46% by volume of R-134a.
• the reactor tube was initially heated to a temperature of 400° C. and during the course of the experiment this temperature was increased in stages to 450° C., 475° C. and then finally to 500° C. At each temperature, a sample of the gaseous product stream emerging from the scrubber was collected and analysed once the system had equilibriated.

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• 1995
  • 1995-07-31 EP EP95927042A patent/EP0775100B1/en not_active Expired - Lifetime
  • 1995-07-31 WO PCT/GB1995/001799 patent/WO1996005157A1/en not_active Ceased
  • 1995-07-31 US US08/776,644 patent/US5856593A/en not_active Expired - Fee Related
  • 1995-07-31 JP JP8507091A patent/JPH10505337A/ja active Pending
  • 1995-07-31 DE DE69519379T patent/DE69519379T2/de not_active Expired - Lifetime
  • 1995-07-31 DK DK95927042T patent/DK0775100T3/da active

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